CN203768311U - Delayed coking device - Google Patents
Delayed coking device Download PDFInfo
- Publication number
- CN203768311U CN203768311U CN201420058826.9U CN201420058826U CN203768311U CN 203768311 U CN203768311 U CN 203768311U CN 201420058826 U CN201420058826 U CN 201420058826U CN 203768311 U CN203768311 U CN 203768311U
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- Prior art keywords
- thermal cracking
- coking
- radiation section
- oil
- cracking reactor
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- Expired - Lifetime
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- 238000004939 coking Methods 0.000 title claims abstract description 68
- 230000003111 delayed effect Effects 0.000 title claims abstract description 25
- 238000004227 thermal cracking Methods 0.000 claims abstract description 41
- 239000000571 coke Substances 0.000 claims abstract description 34
- 230000005855 radiation Effects 0.000 claims abstract description 33
- 238000010438 heat treatment Methods 0.000 claims abstract description 14
- 238000000034 method Methods 0.000 claims description 42
- 238000004508 fractional distillation Methods 0.000 claims description 32
- 238000005516 engineering process Methods 0.000 abstract description 5
- 238000005504 petroleum refining Methods 0.000 abstract 1
- 239000003921 oil Substances 0.000 description 58
- 238000006243 chemical reaction Methods 0.000 description 24
- 238000005336 cracking Methods 0.000 description 20
- 239000007789 gas Substances 0.000 description 20
- 239000007788 liquid Substances 0.000 description 12
- 239000000295 fuel oil Substances 0.000 description 10
- 238000005406 washing Methods 0.000 description 8
- 238000000926 separation method Methods 0.000 description 7
- 239000000203 mixture Substances 0.000 description 5
- 238000007701 flash-distillation Methods 0.000 description 4
- 239000010426 asphalt Substances 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000012263 liquid product Substances 0.000 description 3
- 239000003208 petroleum Substances 0.000 description 3
- 230000001698 pyrogenic effect Effects 0.000 description 3
- 238000007670 refining Methods 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 239000011280 coal tar Substances 0.000 description 2
- 238000005194 fractionation Methods 0.000 description 2
- 239000003502 gasoline Substances 0.000 description 2
- 229910001385 heavy metal Inorganic materials 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003610 charcoal Substances 0.000 description 1
- 239000007795 chemical reaction product Substances 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000004231 fluid catalytic cracking Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 230000035800 maturation Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003079 shale oil Substances 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
Abstract
The utility model discloses a delayed coking device in the field of petroleum refining, and aims at solving the problems that the operation of a viscosity-breaking reactor is fluctuant when switching the operation of a coke drum in the existing delayed coking technology, and the like. The delayed coking device is provided with a heating furnace (1), a shallow thermal cracking reactor (2), a coke drum, a coking fractionating column (4), a heavy coking wax oil pump (5) and a feed pump (6) of a radiation section, wherein a transfer line (12) of the shallow thermal cracking reactor is arranged between the upper part of the shallow thermal cracking reactor and the lower part of the coking fractionating column; a bottom outlet pipe (13) of the fractionating column is arranged between the bottom of the coking fractionating column and the inlet of the feed pump of the radiation section; an outlet pipe (14) of the feed pump of the radiation section is arranged between the outlet of the feed pump (6) of the radiation section and the inlet of a furnace pipe of the radiation section of the heating furnace. By using the delayed coking device, the operation of the shallow thermal cracking reactor is not fluctuant basically when the operation of the coke drum is switched so as to maintain stable operation.
Description
Technical field
The utility model relates to a kind of delayed coking unit in refining of petroleum field.
Background technology
Delay coking process because de-charcoal is thorough, flow process is simple, technology maturation, plant investment be relatively low, especially can process the inferior heavy oil of high carbon residue, high bituminous matter, high heavy metal content, therefore be subject to the generally attention of oil refining enterprise, and become one of technique with fastest developing speed of heavy oil upgrading in recent years.Although delay coking process, having certain technical superiority aspect processing inferior heavy oil, because following the low value-added gas of output and coke, therefore makes the utilization ratio of petroleum resources lower compared with heavy oil hydrogenation process.And, along with the further variation of processing heavy oil character (it is large that density becomes, and viscosity, carbon residue, heavy metal and asphalt content improve), not only make the cycle of operation of device shorten, and output more gas and coke.For addressing the above problem, refining of petroleum investigator has developed some relevant technology.
Chinese patent CN101597518A discloses a kind of improved delay coking process, it is characterized in that, charging enters dehesion reactor after heating in process furnace convection zone and carries out cracking reaction, the isolated heavy oil of reaction product enters coke drum after heating in process furnace radiation section, and the oil gas that goes out coke drum and dehesion gas reactor are separately or after mixing, enter coking fractional distillation column and carry out fractionation.This invention can improve production efficiency of delayed coking liquid product, reduces coking yield, extends delayed coking unit on-stream time.The problem existing is: (1) coke drum is in the time of blocked operation, can along pipeline, process furnace radiant coil, process furnace radiation section and gas-liquid separator between coke drum bottom and process furnace radiation section or and gas-liquid separation zone, dehesion reactor top between pipeline, the quiet run of gas-liquid separation and dehesion reactor is exerted an influence.Because the cushioning pocket along described path is little, dehesion reactor will there will be operation fluctuation (for example fluctuation of the residence time, pressure), make dehesion reaction not reach due effect.And the operation fluctuation that prior art occurs dehesion reactor lacks solution.(2) need at the outer setting gas-liquid separator of dehesion reactor or the top within dehesion reactor arrange gas-liquid separation zone, increase facility investment.
Summary of the invention
The purpose of this utility model is to provide a kind of delayed coking unit, can make when the blocked operation dehesion reactor occur operation fluctuation, on dehesion reactor outer setting gas-liquid separator or the top within dehesion reactor, gas-liquid separation zone is set and has increased the problem of facility investment to solve the existing coke drum of existing Delayed Coking Technology.
For addressing the above problem, the technical solution adopted in the utility model is: a kind of delayed coking unit, be provided with process furnace, shallow degree thermal cracking reactor, coke drum, coking fractional distillation column, heavy wax tailings pump, in process furnace, be provided with heating tube in section of convection chamber, radiant coil, between the outlet of heating tube in section of convection chamber and shallow degree thermal cracking reactor, be provided with convection zone outlet pipe, between the outlet of radiant coil and the bottom of coke drum, be provided with process furnace radiation section outlet pipe, between the top of coke drum and the bottom of coking fractional distillation column, be provided with main oil gas piping, heavy wax tailings pump outlet is provided with heavy wax tailings pump discharge pipe, it is characterized in that: between the top of shallow degree thermal cracking reactor and the bottom of coking fractional distillation column, be provided with shallow degree thermal cracking reactor transfer line, delayed coking unit is provided with radiation section fresh feed pump, between the entrance of the bottom of coking fractional distillation column and radiation section fresh feed pump, be provided with Fractionator Bottom outlet pipe, between radiation section charging pump outlet and the entrance of radiant coil, be provided with radiation section fresh feed pump outlet pipe.
Adopt the utility model, there is following beneficial effect: (1) coke drum, in the time of blocked operation, can cause operation fluctuation to the bottom of coking fractional distillation column along the path of process furnace radiation section outlet pipe, process furnace radiant coil, radiation section fresh feed pump outlet pipe, radiation section fresh feed pump, Fractionator Bottom outlet pipe.But because the space of coking fractional distillation column bottom is very large, can provide enough cushioning pockets to alleviate described operation fluctuation, be delivered to shallow degree thermal cracking reactor, the quiet run of shallow degree thermal cracking reactor is produced to larger impact along shallow degree thermal cracking reactor transfer line so generally do not have larger operation fluctuation.Therefore, coke drum shallow degree thermal cracking reactor in the time of blocked operation there will not be operation fluctuation substantially, can maintain quiet run, reach due shallow degree heat cracking reaction effect.In addition, for the operation fluctuation of coking fractional distillation column, industrially can control with comparalive ease and solve by a lot of methods.(2) the utility model need at the outer setting gas-liquid separator of shallow degree thermal cracking reactor or the top within shallow degree thermal cracking reactor arrange gas-liquid separation zone, has reduced facility investment.(3) the utility model is in operating process, heavy, inferior feedstock oil remain and in shallow degree thermal cracking reactor, carry out entering coke drum after shallow degree heat cracking reaction again and carry out pyrogenic reaction, shallow degree thermal cracking process and degree of depth thermal cracking process are organically combined togather, can obtain equally reduction delayed coking gas and coke yield, raising liquid product (especially coker gas oil) productive rate, slow down the useful technique effect such as e-quipment and pipe coking, the extension fixture cycle of operation.
Below in conjunction with the drawings and specific embodiments, the utility model is described in further detail.The drawings and specific embodiments do not limit the claimed scope of the utility model.
Brief description of the drawings
Fig. 1 is the schematic diagram of the utility model delayed coking unit.
Embodiment
Referring to Fig. 1, delayed coking unit of the present utility model is provided with process furnace 1, shallow degree thermal cracking reactor 2, coke drum (comprising the first coke drum 31, the second coke drum 32), coking fractional distillation column 4, heavy wax tailings pump 5.In process furnace 1, be provided with heating tube in section of convection chamber, radiant coil.Heating tube in section of convection chamber can be all located in the convection zone of process furnace 1, also can major part be located in the convection zone of process furnace 1, small portion is located in the radiation section of process furnace 1; Radiant coil is all located in the radiation section of process furnace 1.The entrance of heating tube in section of convection chamber is connected with raw material oil pipe 7, between outlet and shallow degree thermal cracking reactor 2, is provided with convection zone outlet pipe 11.The outlet of convection zone outlet pipe 11 can be connected in top or bottom (being to be connected in bottom shown in Fig. 1) of shallow degree thermal cracking reactor 2.Between the outlet of radiant coil and the bottom of coke drum, be provided with process furnace radiation section outlet pipe 15, between the top of coke drum and the bottom of coking fractional distillation column 4, be provided with main oil gas piping 16.The bottom of coking fractional distillation column 4 is provided with heavy wax tailings oil header 22, and the top of heavy wax tailings oil header 22 is provided with baffle plate, and the top of baffle plate is provided with washing oil sparger 20; The outlet of main oil gas piping 16 is connected in the region above heavy wax tailings oil header 22 and between below baffle plate with coking fractional distillation column 4.
Between the bottom of the top of shallow degree thermal cracking reactor 2 and coking fractional distillation column 4, be provided with shallow degree thermal cracking reactor transfer line 12, the outlet of shallow degree thermal cracking reactor transfer line 12 is connected with the region that coking fractional distillation column 4 is positioned at heavy wax tailings oil header 22 belows.Delayed coking unit is provided with radiation section fresh feed pump 6; Between the entrance of the bottom of coking fractional distillation column 4 and radiation section fresh feed pump 6, be provided with Fractionator Bottom outlet pipe 13, between the outlet of radiation section fresh feed pump 6 and the entrance of process furnace 1 radiant coil, be provided with radiation section fresh feed pump outlet pipe 14.
Between the outlet of the interior heavy wax tailings oil header 22 of coking fractional distillation column 4 and the entrance of heavy wax tailings pump 5, be provided with heavy wax tailings and extract pipe 9 out, the outlet of heavy wax tailings pump 5 is provided with heavy wax tailings pump discharge pipe 17.The outlet of heavy wax tailings pump discharge pipe 17 is connected with the entrance of heavy wax tailings vent pipe 18, washing oil pipe 19 respectively, and the outlet of washing oil pipe 19 is connected with the washing oil sparger 20 in coking fractional distillation column 4.
Between heavy wax tailings pump discharge pipe 17 and shallow degree thermal cracking reactor transfer line 12, heavy wax tailings circulation tube 21 can be set.
Shallow degree thermal cracking reactor 2 described in the utility model is equivalent to dehesion reactor, and type is generally tower reactor or shell and tube reactor.Shallow degree thermal cracking reactor 2 can arrange 1 (as shown in Figure 1) or more than 2.When multiple shallow degree thermal cracking reactor 2 is set, can adopt the form of serial or parallel connection to connect.
On the delayed coking unit shown in the utility model Fig. 1, carry out the method for delayed coking, comprise the following steps: after the lateral line withdrawal function product heat exchange of stock oil 70 and coking fractional distillation column 4, pump up (figure slightly), heating tube in section of convection chamber in raw material oil pipe 7 enters process furnace 1, in the convection zone of process furnace 1, after heating, flowed out by the outlet of heating tube in section of convection chamber, in convection zone outlet pipe 11 enters shallow degree thermal cracking reactor 2, carry out shallow degree heat cracking reaction.The temperature of shallow degree heat cracking reaction is 360～430 DEG C (being preferably 370～400 DEG C), the cold oil residence time of stock oil 70 in shallow degree thermal cracking reactor 2 is 15～120min (being preferably 30～90min), the top pressure of shallow degree thermal cracking reactor 2 is 0.2～2.5MPa, and the dehesion rate that shallow degree heat cracking reaction generates heavy oil is 10%～95%.Shallow degree heat cracking reaction generates heavy oil, refers to shallow degree heat cracking reaction and generates 200 DEG C of above cuts in oil (seeing below described).Described dehesion rate refers to the viscosity of stock oil 70 at 100 DEG C and the difference percentage ratio that the viscosity at 100 DEG C obtains divided by stock oil 70 of the viscosity of shallow degree heat cracking reaction generation heavy oil at 100 DEG C, and viscosity unit is mm
2/ s.The described cold oil residence time, refer to that stock oil 70 is by the residence time of 20 DEG C of calculating.Pressure described in the utility model is gauge pressure.
Flash distillation is carried out in the bottom (coking fractional distillation column 4 is positioned at the region of heavy wax tailings oil header 22 belows) that shallow degree heat cracking reaction generation oil gas enters coking fractional distillation column 4 through shallow degree thermal cracking reactor transfer line 12, make gas-liquid separation, obtain shallow degree heat cracking reaction and generate oil and shallow degree heat cracking reaction generation gas, flow downwards and upwards respectively.Shallow degree heat cracking reaction generates the oily bottom that comes together in coking fractional distillation column 4.
Referring to Fig. 1, the heavy wax tailings 90 in heavy wax tailings oil header 22 is extracted pipe 9 out through heavy wax tailings and is extracted out by heavy wax tailings pump 5, enters heavy wax tailings pump discharge pipe 17.In the time that the utility model delayed coking unit arranges heavy wax tailings circulation tube 21, can be using heavy part wax tailings 90 as turning oil in heavy wax tailings circulation tube 21 be sent into shallow degree thermal cracking reactor transfer line 12, flash distillation is carried out in the bottom (coking fractional distillation column 4 is positioned at the region of heavy wax tailings oil header 22 belows) that enters coking fractional distillation column 4 together with after generating air-fuel mixture with shallow degree heat cracking reaction, makes gas-liquid separation.The gas obtaining after flash distillation, for shallow degree heat cracking reaction generates gas; The liquid obtaining after flash distillation, for shallow degree heat cracking reaction generates mixture oily and heavy wax tailings 90, comes together in the bottom of coking fractional distillation column 4.
Shallow degree heat cracking reaction generates oil or shallow degree heat cracking reaction generation oil is extracted out by radiation section fresh feed pump 6 through Fractionator Bottom outlet pipe 13 by the bottom of coking fractional distillation column 4 with the mixture of heavy wax tailings 90, the radiant coil entering in process furnace 1 through radiation section fresh feed pump outlet pipe 14 again, be heated to 480～515 DEG C of coking temperatures in the radiation section of process furnace 1 after, flowed out by the outlet of radiant coil, enter coke drum (the first coke drum 31 or the second coke drum 32) through process furnace radiation section outlet pipe 15 and carry out pyrogenic reaction (degree of depth heat cracking reaction); The first coke drum 31 and the second coke drum 32 are taken turns flow operation.Pyrogenic reaction generates oil gas and after chilling, (schemes to omit) bottom (coking fractional distillation column 4 is in the region above heavy wax tailings oil header 22 and between below baffle plate) that enters coking fractional distillation column 4 through main oil gas piping 16, together with generating gas with shallow degree heat cracking reaction, in coking fractional distillation column 4, carry out fractionation, obtain the products such as gas, coker gasoline, coker gas oil, light wax tailings, heavy wax tailings.
Heavy wax tailings 90 (disregarding the part that can circulate in heavy wax tailings circulation tube 21 is sent into shallow degree thermal cracking reactor transfer line 12) in heavy wax tailings pump discharge pipe 17 flows to the outlet of heavy wax tailings pump discharge pipe 17, enters respectively heavy wax tailings vent pipe 18, washing oil pipe 19.The heavy wax tailings that enters heavy wax tailings vent pipe 18 is discharged (Reference numeral 91 represents the heavy wax tailings of discharging), can be used as that turning oil mixes with fresh feed, constitutive material oil 70.Enter the heavy wax tailings of washing oil pipe 19 as washing oil, enter washing oil sparger 20 and spray downwards, in subtend, mobile gas washs with cooling.
In Fig. 1, Reference numeral 8 represents light wax tailings, and the cut point of itself and heavy wax tailings is 420～530 DEG C.Reference numeral 10 represents the coke that coke drum generates.
The stock oil 70 of the utility model processing can be fresh feed, can be also the mixture of fresh feed and various turning oils.Fresh feed is from one or more the mixture in the vacuum residuum of external process device, long residuum, heavy crude, de-oiled asphalt, residual hydrogenation heavy oil, thermal cracking residue, decompressed wax oil, extraction oil, catalytic slurry, ethylene bottom oil, shale oil, coal tar, tar-bitumen etc.Turning oil is the self-produced heavy wax tailings 90 of the utility model delayed coking unit, light wax tailings 8, coker gas oil, coker gasoline, or from the oil plant of other oil-processing units, such as fluid catalytic cracking decant oil, coal tar light constituent (400 DEG C of following cuts) etc., can select one or more uses wherein.The quality (referring to the total mass of various turning oils while using two or more turning oil) of turning oil and the mass ratio (recycle ratio) of fresh feed, be generally 0～1.
For slow down coking, in operating process, can locate to inject appropriate water vapor to bottom, the radiant coil etc. of shallow degree thermal cracking reactor 2.The water vapor amount of wherein injecting to shallow degree thermal cracking reactor 2 bottoms is generally the 0～1.5m% (0.2～0.8m% that is preferably stock oil 70 quality, m% represents mass percent) of stock oil 70 quality.In order to improve the yield of delayed coking liquid product, can inject hydrogen supply agent, increase liquor or anticoking agent to a place or a few place among radiant coil, process furnace radiation section outlet pipe 15, the first coke drum 31 tops and the second coke drum 32 tops in process furnace 1.
Claims (2)
1. a delayed coking unit, be provided with process furnace (1), shallow degree thermal cracking reactor (2), coke drum, coking fractional distillation column (4), heavy wax tailings pump (5), process furnace is provided with heating tube in section of convection chamber in (1), radiant coil, between the outlet of heating tube in section of convection chamber and shallow degree thermal cracking reactor (2), be provided with convection zone outlet pipe (11), between the outlet of radiant coil and the bottom of coke drum, be provided with process furnace radiation section outlet pipe (15), between the bottom of the top of coke drum and coking fractional distillation column (4), be provided with main oil gas piping (16), the outlet of heavy wax tailings pump (5) is provided with heavy wax tailings pump discharge pipe (17), it is characterized in that: between the top of shallow degree thermal cracking reactor (2) and the bottom of coking fractional distillation column (4), be provided with shallow degree thermal cracking reactor transfer line (12), delayed coking unit is provided with radiation section fresh feed pump (6), between the entrance of the bottom of coking fractional distillation column (4) and radiation section fresh feed pump (6), be provided with Fractionator Bottom outlet pipe (13), between the outlet of radiation section fresh feed pump (6) and the entrance of radiant coil, be provided with radiation section fresh feed pump outlet pipe (14).
2. delayed coking unit according to claim 1, is characterized in that: between heavy wax tailings pump discharge pipe (17) and shallow degree thermal cracking reactor transfer line (12), be provided with heavy wax tailings circulation tube (21).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420058826.9U CN203768311U (en) | 2014-01-26 | 2014-01-26 | Delayed coking device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201420058826.9U CN203768311U (en) | 2014-01-26 | 2014-01-26 | Delayed coking device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN203768311U true CN203768311U (en) | 2014-08-13 |
Family
ID=51285525
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201420058826.9U Expired - Lifetime CN203768311U (en) | 2014-01-26 | 2014-01-26 | Delayed coking device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN203768311U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106924984A (en) * | 2015-12-30 | 2017-07-07 | 中国石油天然气股份有限公司 | A kind of method for controlling fractionation column bottom liquid level and reaction severity |
-
2014
- 2014-01-26 CN CN201420058826.9U patent/CN203768311U/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106924984A (en) * | 2015-12-30 | 2017-07-07 | 中国石油天然气股份有限公司 | A kind of method for controlling fractionation column bottom liquid level and reaction severity |
| CN106924984B (en) * | 2015-12-30 | 2020-05-08 | 中国石油天然气股份有限公司 | Method for controlling liquid level and reaction severity of tower bottom of fractionating tower |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CX01 | Expiry of patent term | ||
| CX01 | Expiry of patent term |
Granted publication date: 20140813 |